US3967975A - Fluidization apparatus - Google Patents

Fluidization apparatus Download PDF

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Publication number
US3967975A
US3967975A US05/526,784 US52678474A US3967975A US 3967975 A US3967975 A US 3967975A US 52678474 A US52678474 A US 52678474A US 3967975 A US3967975 A US 3967975A
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US
United States
Prior art keywords
chamber
tubes
fluidizing gas
lower chamber
upper chamber
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
US05/526,784
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English (en)
Inventor
Leo R. Idaszak
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Unilever Bestfoods North America
Original Assignee
Unilever Bestfoods North America
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Unilever Bestfoods North America filed Critical Unilever Bestfoods North America
Priority to US05/526,784 priority Critical patent/US3967975A/en
Priority to AR261347A priority patent/AR208418A1/es
Priority to AU86919/75A priority patent/AU495208B2/en
Priority to US05/634,208 priority patent/US4021927A/en
Priority to SE7513172A priority patent/SE408020B/xx
Priority to DK528275AA priority patent/DK153525B/da
Priority to ZA757357A priority patent/ZA757357B/xx
Priority to ES443132A priority patent/ES443132A1/es
Priority to FI753304A priority patent/FI62958C/fi
Priority to SE7513173A priority patent/SE416023B/xx
Priority to CA240,310A priority patent/CA1069275A/fr
Priority to CA240,309A priority patent/CA1069277A/fr
Priority to DK528375A priority patent/DK153526B/da
Priority to ES442913A priority patent/ES442913A1/es
Priority to CH1528875A priority patent/CH620839A5/de
Priority to GB48463/75A priority patent/GB1498206A/en
Priority to GB48464/75A priority patent/GB1482869A/en
Priority to AR26134875A priority patent/AR218215A1/es
Priority to JP50141019A priority patent/JPS5176169A/ja
Priority to CH1528775A priority patent/CH613874A5/xx
Priority to YU2987/75A priority patent/YU37071B/xx
Priority to DE2552891A priority patent/DE2552891C2/de
Priority to DE19752552881 priority patent/DE2552881C2/de
Priority to NL7513763A priority patent/NL173923C/xx
Priority to BE2054672A priority patent/BE835888A/fr
Priority to AT0896675A priority patent/AT369288B/de
Priority to NL7513765A priority patent/NL7513765A/xx
Priority to BR7507802*A priority patent/BR7507802A/pt
Priority to BR7507801A priority patent/BR7507801A/pt
Priority to FR7535963A priority patent/FR2291788A1/fr
Priority to FR7535962A priority patent/FR2291787A1/fr
Priority to BE2054671A priority patent/BE835887A/fr
Priority to JP50141020A priority patent/JPS593200B2/ja
Priority to IT29639/75A priority patent/IT1049867B/it
Priority to IT2964675A priority patent/IT1054911B/it
Priority to AT0896575A priority patent/AT369667B/de
Priority to AU86938/75A priority patent/AU494807B2/en
Priority to HU75CE1066A priority patent/HU173973B/hu
Priority to HU75CE00001065A priority patent/HU171560B/hu
Application granted granted Critical
Publication of US3967975A publication Critical patent/US3967975A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08B—POLYSACCHARIDES; DERIVATIVES THEREOF
    • C08B31/00—Preparation of derivatives of starch
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
    • B01J8/28—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations the one above the other
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/38—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it
    • B01J8/382—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it with a rotatable device only
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08B—POLYSACCHARIDES; DERIVATIVES THEREOF
    • C08B30/00—Preparation of starch, degraded or non-chemically modified starch, amylose, or amylopectin
    • C08B30/12—Degraded, destructured or non-chemically modified starch, e.g. mechanically, enzymatically or by irradiation; Bleaching of starch
    • C08B30/18—Dextrin, e.g. yellow canari, white dextrin, amylodextrin or maltodextrin; Methods of depolymerisation, e.g. by irradiation or mechanically
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D13/00—Heat-exchange apparatus using a fluidised bed
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/16—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged in parallel spaced relation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
    • F28D2021/0019—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for
    • F28D2021/0045—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for for granular materials

Definitions

  • the present invention relates to a fluidization apparatus, and more particularly, to a fluidized bed apparatus for carrying out chemical reactions and/or unit operations.
  • Fluidized bed equipment has been used for years for a variety of purposes, including the carrying out of chemical reactions and/or unit operations such as drying.
  • a solid phase is suspended in an upwardly moving fluid stream, usually a gas stream, whereby the mass of solid particles behaves somewhat like a boiling liquid.
  • the solid phase may be a catalyst to promote a chemical reaction in the stream of fluidizing gas, or it may be a material reactive with the fluidizing gas.
  • the solid phase may be a material which is treated by the fluidizing gas as in the case of fluidized drying.
  • Fluidized bed systems are, however, not without disadvantages.
  • the use of fluidized systems for chemical reactions frequently results in channeling, a phenomenon caused by pockets in the solid phase which results in the passage of gas through the bed without intimate contact with the solid phase.
  • the problem of channeling in a fluidized bed system can be partially minimized by the use of a plurality of tubular zones through which the fluidizing gas is passed in contact with the solid phase.
  • Each tube thus operates as an individual fluidized bed with a much smaller cross sectional area.
  • Such tubular bed systems have even greater heat transfer characteristics because the plurality of tubular zones increase the surface area available for heat transfer.
  • tubular reactors used in dextrinization of starch are frequently characterized by a "dead zone" at the upper portion where the starch may lay and be subjected to high temperatures for extended periods. Auto ignition can occur, causing fire and/or explosions.
  • FIG. 1 is a sectional view of a fluidized apparatus embodying the features of the present invention
  • FIG. 2 is a partial sectional view taken along lines 2--2 in FIG. 1;
  • FIG. 3 is a schematic view of the apparatus of the present invention adapted for use in the conversion of starch to dextrin.
  • the concepts of the present invention reside in a fluidized bed apparatus which is formed of a single elongate, generally upstanding reactor which is divided into three sections. One is an upper chamber at the top portion of the reactor and the other is a lower chamber at the bottom portion of the reactor. Positioned between the upper and lower chambers is a section formed by a plurality of tubes each of which communicate at their upper end with the upper chamber and at their lower end with the lower chamber.
  • the reactor also includes inlet means in the upper chamber to supply a fluidizable material to the upper chamber and outlet means in the lower chamber to remove fluidizable material from the system.
  • the fluidizing gas is introduced through inlet means in the lower chamber and passes upwardly through the lower chamber, through the plurality of tubes and into the upper chamber while fluidizing the fluidizable material in the lower chamber, the tubes and the upper chamber.
  • both the upper and lower chambers are provided with agitation means to further insure vigorous mixing in both the upper and lower chambers. In this way, channeling in the upper and lower chambers is virtually eliminated.
  • the fluidizable material thus introduced to the upper chamber flows by gravity downwardly from the upper chamber, through the plurality of tubes and into the lower chamber from which it is discharged from the apparatus.
  • the solid phase or fluidizable material thus flows by gravity countercurrent to the fluidizing gas, and passes slowly by gravity against the action of the suspending or fluidizing medium.
  • the apparatus of the present invention is ideally suited for use in the conversion of starch to dextrin.
  • the apparatus of this invention is likewise suitable for a variety of other fluidized bed applications including fluidized drying, petroleum cracking operations and the like where fluidized bed systems have been used in the past.
  • the apparatus of the invention will hereinafter be described in conjunction with the conversion of starch to dextrin, with the understanding that it may similarly be used for many other fluidized operations.
  • the apparatus includes an elongate vertical housing designated as 10 which defines in its upper portion, an upper chamber 12 having inlet means 14 to supply a fluidizable material thereto.
  • the housing 10 also defines a lower chamber 16 positioned at substantially the bottom.
  • Both of the upper chamber 12 and the lower chamber 16 include agitator means 18 and 20, respectively.
  • the agitator means 18 includes a shaft 22 mounted for rotation within the upper chamber 12.
  • Mounted on shaft 22 for rotation therewith are a plurality of blades 24 which may be in the form of flat paddles rotatable with the shaft 22.
  • the agitator means 20 in the lower chamber 16 similarly includes a rotatable shaft 26 having substantially flat blades 28 mounted for rotation therewith.
  • the agitating means 18 is formed with flat blades 24 at staggered locations, with additional flat blades 30 being mounted at a 90° angle between each of the blades 24. These blades present a substantially flat surface lying in a plane transverse to the direction of flow of the fluidizing gas.
  • the agitating means 20 in the lower chamber 16 preferably has a similar configuration. If desired, some or all of the blades can be disposed at angle with respect to those illustrated.
  • a plurality of tubes 34 Positioned in the housing 10 in an intermediate section 32 are a plurality of tubes 34 having an upper end 36 communicating with the upper chamber 12 and a lower end 38 communicating with the lower chamber 16. In this way, fluidizable material introduced to the inlet 14 flows by gravity downwardly through the upper chamber 12 through the plurality of tubes 34 and into the lower chamber 16.
  • the lower chamber 16 also includes outlet means 40 to withdraw fluidizable material therefrom.
  • Fluidizing gas is introduced to the plenum chamber through fluidizing gas inlet means 46, and passes through a foraminous distributor plate 48 into the lower chamber 16.
  • the arrangement of the tubes in the intermediate section 32 can be varied considerably.
  • One suitable arrangement for the tubes 34 in the section 32 is shown in FIG. 2 of the drawing. As shown in this figure, the tubes 34 are arranged in a pattern about the center of the section 32.
  • the tubular section is provided with means to supply and/or remove heat therefrom.
  • the section 32 preferably defines a jacket for heat exchange media which can be supplied to the section 32 by inlet means 49 and removed from the section or jacket 32 by outlet means 50 as shown in FIG. 1. It is also desirable in many instances to employ heat exchange means with the upper and lower chambers. For this purpose, it is generally sufficient to provide a jacket 52 surrounding the upper chamber 12, with the jacket 52 including inlet means 54 to supply heat exchange media to the jacket 52 and outlet means 56 to remove heat exchange media from the jacket 52.
  • the heat exchange jacket 52 for the upper chamber 12 extend only up to the inlet means 14.
  • the upper chamber 12 include a dome portion 58 integral therewith from which the fluidizing gas may be removed from the reactor by means of outlet means 60.
  • the fluidizing gas may be removed from the reactor by means of outlet means 60.
  • the fluidizing gas not only is the fluidizing gas removed from the outlet means 60, but any "fines" entrained in the fluidizing gas are carried out with it through the outlet means 60.
  • the cross sectional area of the dome itself may be increased, or, the cross sectional area of the entire chamber 12 may be increased for this purpose.
  • the lower chamber 16 may likewise be provided with heat exchange media, preferably in the form of a jacket 62, to which heat exchange media is supplied through inlet means 64 and from which the heat exchange media can be removed from outlet means 66.
  • FIG. 3 of the drawing The apparatus of the present invention adapted for use in the conversion of starches to dextrin is shown in FIG. 3 of the drawing.
  • the supply of starch preferably containing an acid catalyst
  • the inlet means 14 for introduction to the upper chamber 12.
  • steam is introduced through 72 and 74 into the heat exchange jacket 52 to supply heat to the upper chamber.
  • the shaft 22 of the agitating means 18 can be driven by suitable means 76 as shown in FIG. 3.
  • the catalyst-containing starch is fluidized by humid air introduced to the plenum chamber 44 through the inlet means 46 and passes upwardly through the lower chamber 16, through the tubes 34 in the intermediate section 32 and into the upper chamber 12. Steam as a heat exchange medium is also supplied through lines 78 to the jacket of section 32, and also through line 80 to the jacket 62 surrounding the lower chamber 16. In this way, the upper and lower chambers as well as the tubular section are supplied with steam to heat the starch passing therethrough.
  • the acidified starch supplied to the inlet means 14 is immediately fluidized in the upper chamber 12 while the upper chamber 12 is continuously agitated by the blades 24 and 30.
  • the starch slowly flows by gravity against the action of the fluidizing medium downwardly through the upper chamber while subjected to agitation.
  • the acidified starch continues its downward flow by gravity against the suspending action of the air through the tubes 34 in which there is no agitation, except for that which occurs naturally due to the inherent turbulence in the tubes containing the fluidized starch.
  • the starch After descending through the tubes 34, the starch, at least partially converted to dextrin, continues its descent into the lower chamber 16 again against the action of the heated air, and it is removed from the lower chamber 16 through the outlet means 40.
  • the product removed through line 40 is passed through a rotary air lock 82 into a pneumatic cooling tube where the temperature of the product is lowered to below 150°F.
  • the product is discharged through the rotary air lock 82 into the cooling tube 84 and to collect equipment through line 86. Dust or fines discharged through the discharge means 60 is removed by means of a cyclone 88, and is thus transported by dust discharge line 90 to the collection equipment through line 86.
  • the starch is blended with an acid catalyst, preferably HCl, for supply to the fluidized bed reactor of the invention.
  • an acid catalyst preferably HCl
  • the acidified starch is then passed through the apparatus while maintained at a temperature which is dependent somewhat on the type of dextrin to be produced.
  • the starch is maintained at a temperature within the range of 125°-380°F, and preferably 170°-375°F in the fluidized bed reactor.
  • the residence time of the starch in the fluidized bed reactor of this invention is less than one hour, and most frequently ranges from 10 to 30 minutes, although longer or shorter residence times may be employed depending somewhat on the grade of dextrin desired and the degree of conversion sought.
  • the air as the fluidizing gas may be heated, depending on the grade of dextrin to be produced.
  • the air can be heated to a temperature within the range from 85°F to 350°F.
  • temperatures within the range of 225°-310°F are usually preferred.
  • the air supplied as the fluidizing gas preferably contains moisture to more efficiently promote the conversion reaction.
  • the air should have a relative humidity within the range of 15 to 80%, depending, again, on the grade of dextrin to be produced and the temperature of the air. In this way, the introduction of water and/or acid catalyst directly onto the starch in the fluid bed reactor can be avoided, thereby further reducing any tendency for the starch to agglomerate.
  • fluidizing media can be used.
  • steam, or inert gases such as nitrogen, carbon dioxide, etc., preferably containing some moisture can be used.
  • flue gases from combustion operations can similarly be used as the fluidizing medium if desired. It is not essential that the fluidizing medium add any sensible heat to the starch undergoing dextrinization since the tubular section of the reactor employed with the concepts in the practice of this invention in the dextrinization of starches is capable of providing all of the heat necessary to efficiently effect the reaction.
  • This example illustrates the use of a fluidized bed reactor of the type illustrated in FIGS. 1 and 3 of the drawing, having 7 tubes in the intermediate section.
  • An acidified starch is prepared by feeding raw starch to a covered ribbon blender to which gaseous hydrochloric acid is subsequently added.
  • the amount of hydrochloric acid added is determined by titration and it is reported as a titer which represents the milliliters of 0.1 N NaOH required to bring 20 grams of starch slurried in 100 milliliters of distilled water to a pH of 6.
  • the acidified starch is introduced to the fluidized bed through the inlet means 14, and air is introduced to the plenum chamber 44.
  • Dextrins may be characterized as either white dextrins or canary dextrins. Further, white dextrins may be either high solubles or low solubles. Solubles are reported as per cent, and represents the amount of a 2-gram sample which dissolves after being suspended in 250 milliliters of water at 25°C and shaken for 1 hour.
  • Canary dextrins are classified as either thick (high viscosity) or thin (low viscosity).
  • Dextrin viscosity is normally reported as fluidity.
  • a 3:4 fluidity such as for Test 4050 in the table below, represents the following.
  • Three parts by weight of dextrin sample are mixed with four parts by weight of water, heated in a steam bath for 30 minutes, then cooled to 25°C. Any evaporation of water, as determined by weighing, is compensated for by addition of water.
  • the material is then strained through a No. 5029 nylon into a glass beaker and held at 25°C for a total cooling time of 1 hour.
  • the material is then placed in a standard funnel at 25°C.
  • Fluidity is normally reported in units of milliliters and represents the amount of material that flows out of the standard funnel in exactly 70 seconds.
  • the borax fluidity method is the same as that described above, except that 10% by weight of the sample is substituted with borax (Na 2 B 4 O 7 .10H 2 O).
  • the fluid bed apparatus contained 7 tubes, the tubes have an inside diameter of 2.834 inches.
  • the height of each tube was 5 feet.
  • the apparatus of the invention can be used for other fluidized bed operations. It will be appreciated by those skilled in the art that the feed and discharge arrangements of the apparatus as described herein may be reversed whereby the material to be fluidized is fed to the bottom of the reactor and the solid material to be recovered is removed from the top of the reactor.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • General Engineering & Computer Science (AREA)
  • Biochemistry (AREA)
  • Thermal Sciences (AREA)
  • Mechanical Engineering (AREA)
  • Combustion & Propulsion (AREA)
  • Polymers & Plastics (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Materials Engineering (AREA)
  • Health & Medical Sciences (AREA)
  • Medicinal Chemistry (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Polysaccharides And Polysaccharide Derivatives (AREA)
  • Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
US05/526,784 1974-11-25 1974-11-25 Fluidization apparatus Expired - Lifetime US3967975A (en)

Priority Applications (39)

Application Number Priority Date Filing Date Title
US05/526,784 US3967975A (en) 1974-11-25 1974-11-25 Fluidization apparatus
AR261347A AR208418A1 (es) 1974-11-25 1975-01-01 Aparato para ilevar a cabo operaciones f uidificadas
AU86919/75A AU495208B2 (en) 1974-11-25 1975-11-02 Fluidization apparatus
US05/634,208 US4021927A (en) 1974-11-25 1975-11-21 Process for fluidization
SE7513172A SE408020B (sv) 1974-11-25 1975-11-24 Fluidiseringsanordning
ZA757357A ZA757357B (en) 1974-11-25 1975-11-24 Process for fluidization
ES443132A ES443132A1 (es) 1974-11-25 1975-11-24 Un procedimiento de fluidificacion numero 634.208 para la fluidificacion de solidos.
FI753304A FI62958C (fi) 1974-11-25 1975-11-24 Anordning foer utfoerande av fluidiseringsprocesser
SE7513173A SE416023B (sv) 1974-11-25 1975-11-24 Fluidiseringsforfarande
CA240,310A CA1069275A (fr) 1974-11-25 1975-11-24 Methode de fluidification
CA240,309A CA1069277A (fr) 1974-11-25 1975-11-24 Appareil de fluidisation
DK528375A DK153526B (da) 1974-11-25 1975-11-24 Fluidiseringsfremgangsmaade, isaer til brug paa vanskeligt fluidiserbare materialer
ES442913A ES442913A1 (es) 1974-11-25 1975-11-24 Aparato de reaccion perfeccionado.
DK528275AA DK153525B (da) 1974-11-25 1975-11-24 Fluidiseringsapparat
FR7535963A FR2291788A1 (fr) 1974-11-25 1975-11-25 Procede de fluidisation par un gaz de matieres solides, notamment l'amidon
GB48464/75A GB1482869A (en) 1974-11-25 1975-11-25 Fluidization apparatus
AR26134875A AR218215A1 (es) 1974-11-25 1975-11-25 Procedimiento de fluidificacion para la preparacion de derivados de almidon
JP50141019A JPS5176169A (fr) 1974-11-25 1975-11-25
CH1528775A CH613874A5 (fr) 1974-11-25 1975-11-25
YU2987/75A YU37071B (en) 1974-11-25 1975-11-25 Fluidification device
CH1528875A CH620839A5 (en) 1974-11-25 1975-11-25 Method for fluidising solids
DE19752552881 DE2552881C2 (de) 1974-11-25 1975-11-25 Verfahren zum Fluidisieren von Feststoffen
NL7513763A NL173923C (nl) 1974-11-25 1975-11-25 Werkwijze voor het behandelen van zetmeel in een fluidisatiebed.
BE2054672A BE835888A (fr) 1974-11-25 1975-11-25 Procede de fluidisation par un gaz de matieres solides, notamment l'amidon
AT0896675A AT369288B (de) 1974-11-25 1975-11-25 Fliessbettverfahren
NL7513765A NL7513765A (nl) 1974-11-25 1975-11-25 Fluidiseerinrichting.
BR7507802*A BR7507802A (pt) 1974-11-25 1975-11-25 Aparelho para formacao de um reator
BR7507801A BR7507801A (pt) 1974-11-25 1975-11-25 Processo de fluidificacao
GB48463/75A GB1498206A (en) 1974-11-25 1975-11-25 Process for fluidization
FR7535962A FR2291787A1 (fr) 1974-11-25 1975-11-25 Appareil de fluidisation a tubes d'echange de chaleur pour reactions chimiques
BE2054671A BE835887A (fr) 1974-11-25 1975-11-25 Appareil de fluidisation a buse d'echange de chaleur pour recations chimiques
JP50141020A JPS593200B2 (ja) 1974-11-25 1975-11-25 リユウドウカホウ
IT29639/75A IT1049867B (it) 1974-11-25 1975-11-25 Apparecchio di fluidizzazione
IT2964675A IT1054911B (it) 1974-11-25 1975-11-25 Procedimento per fluidificazione
AT0896575A AT369667B (de) 1974-11-25 1975-11-25 Wirbelschichtreaktor
AU86938/75A AU494807B2 (en) 1975-11-25 Process for fluidization
HU75CE1066A HU173973B (hu) 1974-11-25 1975-11-25 Fluidizacija dlja khimicheskikh i fizicheskikh processov
HU75CE00001065A HU171560B (hu) 1974-11-25 1975-11-25 Ustrojstvo dlja fljuidizacii
DE2552891A DE2552891C2 (de) 1974-11-25 1975-11-25 Verwendung einer Vorrichtung zur Behandlung von Stärke

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US05/526,784 US3967975A (en) 1974-11-25 1974-11-25 Fluidization apparatus

Related Child Applications (1)

Application Number Title Priority Date Filing Date
US05/634,208 Continuation-In-Part US4021927A (en) 1974-11-25 1975-11-21 Process for fluidization

Publications (1)

Publication Number Publication Date
US3967975A true US3967975A (en) 1976-07-06

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Family Applications (1)

Application Number Title Priority Date Filing Date
US05/526,784 Expired - Lifetime US3967975A (en) 1974-11-25 1974-11-25 Fluidization apparatus

Country Status (20)

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US (1) US3967975A (fr)
JP (1) JPS5176169A (fr)
AR (1) AR208418A1 (fr)
AT (2) AT369288B (fr)
BE (2) BE835888A (fr)
BR (1) BR7507802A (fr)
CA (1) CA1069277A (fr)
CH (1) CH613874A5 (fr)
DE (1) DE2552891C2 (fr)
DK (1) DK153525B (fr)
ES (1) ES442913A1 (fr)
FI (1) FI62958C (fr)
FR (1) FR2291787A1 (fr)
GB (2) GB1498206A (fr)
HU (1) HU171560B (fr)
IT (1) IT1049867B (fr)
NL (1) NL7513765A (fr)
SE (1) SE408020B (fr)
YU (1) YU37071B (fr)
ZA (1) ZA757357B (fr)

Cited By (22)

* Cited by examiner, † Cited by third party
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US4075766A (en) * 1976-07-19 1978-02-28 General Signal Corporation Apparatus for the treatment of divided solid material
US4077841A (en) * 1975-07-11 1978-03-07 Klockner-Humboldt-Deutz Aktiengesellschaft Method and apparatus for treating slurries
US4237619A (en) * 1978-12-15 1980-12-09 Cpc International Inc. Fluidized bed apparatus
US4266348A (en) * 1978-12-15 1981-05-12 Cpc International Inc. Fluidized bed process
US4354439A (en) * 1979-06-08 1982-10-19 Babcock-Bsh Ag Vormals Buttner-Schilde-Haas Ag Method of and a device for feeding solid fuel in a fluidized bed hearth
EP0182295A2 (fr) * 1984-11-15 1986-05-28 Cpc International Inc. Poudres pour les soins du corps contenant de l'amidon modifié
US5108713A (en) * 1986-10-15 1992-04-28 The Carborundum Company Apparatus for the continuous production of high ultra-fine, aluminum nitride powder by the carbo-nitridization of alumina
US5641349A (en) * 1995-01-24 1997-06-24 National Starch And Chemical Investment Holding Corporation Water-based adhesives containing thermally-inhibited starches
US5718770A (en) * 1994-08-25 1998-02-17 National Starch And Chemical Investment Holding Corporation Thermally-inhibited pregelatinized granular starches and flours and process for their production
US5725676A (en) * 1993-07-30 1998-03-10 National Starch And Chemical Investment Holding Corporation Thermally inhibited starches and flours and process for their production
US5766366A (en) * 1995-10-13 1998-06-16 A. E. Staley Manufacturing Co. Dry thinned starches, process for producing dry thinned starches, and products and compositions thereof
US5821360A (en) * 1994-01-31 1998-10-13 Henkel Kommanditgesellschaft Auf Aktien Fluidized-bed oxidation process for the production of polysaccharide-based polycarboxylates
US5830884A (en) * 1995-01-18 1998-11-03 National Starch And Chemical Investment Holding Corporation Pharmaceutical products containing thermally-inhibited starches
US5856470A (en) * 1995-03-22 1999-01-05 Henkel Kommanditgesellschaft Auf Aktien Oxidation process for producing polycarboxylates from polysaccharides
US5871756A (en) * 1995-01-18 1999-02-16 National Starch And Chemical Investment Holding Corporation Cosmetics containing thermally-inhibited starches
US5932017A (en) * 1993-07-30 1999-08-03 National Starch And Chemical Investment Holding Corporation Thermally-inhibited non-pregelatinized granular starches and flours and process for their preparation
US6191116B1 (en) 1998-04-27 2001-02-20 National Starch And Chemical Investment Holding Corporation Highly soluble, hydratable, viscous, solution stable pyrodextrins, process of making and use thereof
US6221420B1 (en) 1993-07-30 2001-04-24 National Starch And Chemical Investment Holding Corporation Foods containing thermally-inhibited starches and flours
US6451121B2 (en) 1993-07-30 2002-09-17 National Starch And Chemical Investment Holding Corporation Thermally-inhibited non-pregelatinized granular starches and flours and process for their preparation
US6482366B1 (en) * 1996-01-17 2002-11-19 Commonwealth Scientific And Industrial Research Organisation Calcination using liquid metal heat exchange fluid
EP1281721A1 (fr) * 2001-08-03 2003-02-05 National Starch and Chemical Investment Holding Corporation Amidons modifiés thermiquement et leur procédé de preparation
CN103946243A (zh) * 2011-11-18 2014-07-23 罗盖特公司 具有高分子量的部分可溶的糊精

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DK147287C (da) * 1977-01-13 1984-11-05 Danske Sukkerfab Koeler til blandinger af krystaller og krystalliserende vaeske i produktionen af sukker og beslaegtede produkter
IN152345B (fr) * 1979-04-30 1983-12-24 Cpc International Inc
DD215620A1 (de) * 1983-05-18 1984-11-14 Thaelmann Schwermaschbau Veb Vorrichtung zur trocknung thermolabiler zum anbacken neigender produkte
DD215619B1 (de) * 1983-05-18 1987-03-18 Thaelmann Schwermaschbau Veb Verfahren und vorrichtung zur trocknung thermolabiler anbackungsanfaelliger stoffe
DE3430127C2 (de) * 1984-08-16 1987-04-02 Krauss-Maffei AG, 8000 München Vorrichtung zum Trocknen von feinkörnigen Feststoffpartikeln
AT384289B (de) * 1985-04-23 1987-10-27 Waagner Biro Ag Wirbelbetttrockner mit heizflaechen
GB2190485B (en) * 1986-03-27 1990-03-28 Seaford Nominees Pty Ltd Heat exchanger
DE4016043A1 (de) * 1990-05-18 1991-11-21 Krupp Buckau Maschinenbau Gmbh Vorrichtung zur uebertragung von waerme
DE102004041375A1 (de) * 2004-03-24 2005-10-13 Coperion Waeschle Gmbh & Co. Kg Vorrichtung zum Temperieren von Schüttgut

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US2845368A (en) * 1954-05-27 1958-07-29 Staley Mfg Co A E Dextrinization process
US2987487A (en) * 1955-10-14 1961-06-06 Phillips Petroleum Co Catalyst activation
US3411465A (en) * 1966-02-23 1968-11-19 Shirai Takashi Method for incinerating moist materials and an apparatus therefor

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US2240347A (en) * 1938-12-31 1941-04-29 Standard Oil Co Catalytic conversion system
DE1259329B (de) * 1965-12-22 1968-01-25 Dynamit Nobel Ag Verfahren zur Herstellung von Vinylfluorid
NL168717C (nl) * 1970-04-21 Ube Industries Inrichting voor het overdragen van warmte tussen een eerste en een tweede gas met toepassing van een in kringloop gevoerde, fijnverdeelde vaste stof als warmte-overdrachtsmiddel.
CH555700A (de) * 1971-03-11 1974-11-15 Gorodetsky Igor Yakovlevich Kolonnen-stoffaustauschapparat.
GB1365838A (en) * 1972-04-21 1974-09-04 Ibm Data handling system
JPS5029255B2 (fr) * 1972-07-21 1975-09-22
DE2318035C2 (de) * 1973-04-10 1983-11-24 VVB Zucker- und Stärkeindustrie, DDR 4020 Halle Verfahren und Vorrichtung zur Herstellung von Dextrin aus Stärke oder stärkehaltigen Produkten in der Wirbelschicht

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US2845368A (en) * 1954-05-27 1958-07-29 Staley Mfg Co A E Dextrinization process
FR1136059A (fr) * 1954-09-29 1957-05-09 Duintjer Wilkens Meihuizen & C Procédé pour soumettre l'amidon à des traitements chimiques ou physiques
US2987487A (en) * 1955-10-14 1961-06-06 Phillips Petroleum Co Catalyst activation
US3411465A (en) * 1966-02-23 1968-11-19 Shirai Takashi Method for incinerating moist materials and an apparatus therefor

Cited By (27)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4077841A (en) * 1975-07-11 1978-03-07 Klockner-Humboldt-Deutz Aktiengesellschaft Method and apparatus for treating slurries
US4075766A (en) * 1976-07-19 1978-02-28 General Signal Corporation Apparatus for the treatment of divided solid material
US4237619A (en) * 1978-12-15 1980-12-09 Cpc International Inc. Fluidized bed apparatus
US4266348A (en) * 1978-12-15 1981-05-12 Cpc International Inc. Fluidized bed process
US4354439A (en) * 1979-06-08 1982-10-19 Babcock-Bsh Ag Vormals Buttner-Schilde-Haas Ag Method of and a device for feeding solid fuel in a fluidized bed hearth
EP0182295A2 (fr) * 1984-11-15 1986-05-28 Cpc International Inc. Poudres pour les soins du corps contenant de l'amidon modifié
EP0182295A3 (fr) * 1984-11-15 1987-09-02 Cpc International Inc. Poudres pour les soins du corps contenant de l'amidon modifié
US5108713A (en) * 1986-10-15 1992-04-28 The Carborundum Company Apparatus for the continuous production of high ultra-fine, aluminum nitride powder by the carbo-nitridization of alumina
US5932017A (en) * 1993-07-30 1999-08-03 National Starch And Chemical Investment Holding Corporation Thermally-inhibited non-pregelatinized granular starches and flours and process for their preparation
US5725676A (en) * 1993-07-30 1998-03-10 National Starch And Chemical Investment Holding Corporation Thermally inhibited starches and flours and process for their production
US6451121B2 (en) 1993-07-30 2002-09-17 National Starch And Chemical Investment Holding Corporation Thermally-inhibited non-pregelatinized granular starches and flours and process for their preparation
US6221420B1 (en) 1993-07-30 2001-04-24 National Starch And Chemical Investment Holding Corporation Foods containing thermally-inhibited starches and flours
US5821360A (en) * 1994-01-31 1998-10-13 Henkel Kommanditgesellschaft Auf Aktien Fluidized-bed oxidation process for the production of polysaccharide-based polycarboxylates
US5718770A (en) * 1994-08-25 1998-02-17 National Starch And Chemical Investment Holding Corporation Thermally-inhibited pregelatinized granular starches and flours and process for their production
US5830884A (en) * 1995-01-18 1998-11-03 National Starch And Chemical Investment Holding Corporation Pharmaceutical products containing thermally-inhibited starches
US5871756A (en) * 1995-01-18 1999-02-16 National Starch And Chemical Investment Holding Corporation Cosmetics containing thermally-inhibited starches
US5641349A (en) * 1995-01-24 1997-06-24 National Starch And Chemical Investment Holding Corporation Water-based adhesives containing thermally-inhibited starches
US5856470A (en) * 1995-03-22 1999-01-05 Henkel Kommanditgesellschaft Auf Aktien Oxidation process for producing polycarboxylates from polysaccharides
US5817180A (en) * 1995-10-13 1998-10-06 A. E. Staley Manufacturing Dry thinned starches process for producing dry thinned starches and products and compositions thereof
US5766366A (en) * 1995-10-13 1998-06-16 A. E. Staley Manufacturing Co. Dry thinned starches, process for producing dry thinned starches, and products and compositions thereof
US6482366B1 (en) * 1996-01-17 2002-11-19 Commonwealth Scientific And Industrial Research Organisation Calcination using liquid metal heat exchange fluid
US6191116B1 (en) 1998-04-27 2001-02-20 National Starch And Chemical Investment Holding Corporation Highly soluble, hydratable, viscous, solution stable pyrodextrins, process of making and use thereof
EP1281721A1 (fr) * 2001-08-03 2003-02-05 National Starch and Chemical Investment Holding Corporation Amidons modifiés thermiquement et leur procédé de preparation
US20030031775A1 (en) * 2001-08-03 2003-02-13 Altieri Paul A. Thermally converted starches and the method of preparation thereof
US6746705B2 (en) 2001-08-03 2004-06-08 National Starch And Chemical Investment Holding Corporation Thermally converted starches and the method of preparation thereof
CN103946243A (zh) * 2011-11-18 2014-07-23 罗盖特公司 具有高分子量的部分可溶的糊精
US10370553B2 (en) 2011-11-18 2019-08-06 Roquette Freres Partially soluble dextrins of high molecular weight

Also Published As

Publication number Publication date
NL7513765A (nl) 1976-05-28
AU8691975A (en) 1977-06-02
DK528275A (da) 1976-05-26
DK153525B (da) 1988-07-25
IT1049867B (it) 1981-02-10
SE7513172L (sv) 1976-05-26
YU37071B (en) 1984-08-31
CH613874A5 (fr) 1979-10-31
AT369288B (de) 1982-12-27
ES442913A1 (es) 1977-04-01
FI753304A (fr) 1976-05-26
GB1498206A (en) 1978-01-18
BE835888A (fr) 1976-05-25
FI62958C (fi) 1983-04-11
ATA896575A (de) 1982-06-15
FR2291787A1 (fr) 1976-06-18
CA1069277A (fr) 1980-01-08
FR2291787B1 (fr) 1982-05-21
ZA757357B (en) 1976-11-24
ATA896675A (de) 1982-05-15
DE2552891C2 (de) 1985-10-31
BR7507802A (pt) 1976-08-10
YU298775A (en) 1982-06-18
HU171560B (hu) 1978-02-28
DE2552891A1 (de) 1976-05-26
SE408020B (sv) 1979-05-14
FI62958B (fi) 1982-12-31
AR208418A1 (es) 1976-12-27
JPS5176169A (fr) 1976-07-01
BE835887A (fr) 1976-05-25
GB1482869A (en) 1977-08-17
AT369667B (de) 1983-01-25

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